Emulsion polymerization of vinylidene compounds in the presence of trisubstituted hydroperoxymethanes having 10 to 30 carbon atoms



Patented Janiy 5, 1954 EMULSION` POLYMERIZATION" OFA IDENEv vCONIPOUNDS' IN THE PRESEN CE OF TRISUBSTLTUTED 1, HYDROPEROXYMETH- ANES` HAVING T0 30 CARBON ATOMS Wiiiini' B. Reynolds,- John E.

tion of Delaware This invention "relates'to' fan infnxrm'ied'A process' for pol'yrnerizing'unsatiirated organic compounds f While :dispersed fin'a'fi -a'qeous emulsion. 'f In 'one' important `aspectthisfiriverition` relates to the userof` faster recipes 'atlow polymerization temperatures for eiiectingiproduction of synthetic rubber by emulsionlpolyinerizationfof conjugated diolens'. f Thisapplication isiY a continuation-inpart of` our? vco'peridinerapplication Serial No; 68;'73 6,` led Dcenbr'l, 1948.

With" the increasingLinterest in `low tempera-v ture'ernulsion' polymerization; many .variations in recipes and* procedurefhavebeen Ideveloped in the Vinterest of economy andv eciency in addi# tion to the attention given to producing polymeric materials 'having the desiredcharacteristics. Recipes ofthe Aredoxtyp'e",` that is, formulations wherein both oxidizingfand 'reducing components are present, `havefbe'en* Widely used. Oxidizing y' components frequentlyfiemployed include materials of a` peroxidic naturefand particularly come' pouriels suchA as'T benzoyl'f peroxide and 'cu-mene* hydroperoxide: Even?" though any peroxidic material mightJoe'-'expectedl to function inv the capaci-ty' ofthe oxidant in `a'redox emulsion poly-l merization system, this vis'not necessarily thecase since in some'instanes' little; if any,poly`meriza' tionoc'cur's whilev in-otherl cases` with 'dii'ferent factory rate." Some"'proxides :may function fairly' satisfactorilyatffhigher temperatures but are'v of' little Valueiwhen it isf desired to Acarry -out polymerizations` at'lo'w"temperaturesysay below the freezing-'point vof watery We have' now `discovered rthaiffexcellentv con-y Version rat'esv can be obtained ini emulsion poly# merization' -systemsfthroughthe use of initiator,

or catalyst; compositions comprisingla trisub' stituted hydroperoxyniethanehaving at least ten carbon 'atoms Iper molecule. Not 'onlyfare rapid" polymerization rates-'obtained atA low polymeriza-- tion temperatures" with these compositions;vr but uct completely? fr because'ioffadveis'e v1n ogen compounds.'

t and 'cycloolenic radicals. Each vof Vthese radicals '/be"easily'prepared'iby-simple oxidation', with free oxygen; of @the cor-respending" Y hydrocarbon' or hydro'cailoonV4- derivative; i. e.`of the parent tri'- substituted'- methane. l The compound to be oxitemperattire;V and oxl5`1gen--4V introduced at a conc-'f' trolledrat"`th0ihoutfth reaction? period. The mixture is agitated `duringthe reaction which' is'ff generally Y allowed to* continue' ',froni'fabou't oneftol ten ihoursnI The* temperature fein'ployd is pref-'i erahly' maintained between 50 and` 4 160'y Ci," although in some instanesl 'it 'might loefdesirableE to operate,'outs-ide this range, 'that is, at either higher or lower temperatures. Atthe conclusion 4 of -thereactionthe'oxidized mixture' may beeini peroxide composition in the parent compound, or unreacted compound may be stripped and the residual material employed. The major active ingredient in such a composition is the monohydroperoxide, or a mixture of monohydroperoxides. This hydroperoxide group appears to result from introduction of -two oxygen atoms between the carbon atom of the trisubstituted methane and the single hydrogen atom attached thereto. Where there is another similar grouping in the molecule, the usual method of production just outlined appears to produce only the monohydroperoxide even though a dihydroperoxide appears to be structurally possible. Thus, in a simple case, from such an oxidation of diisopropyl benzene the primary product appears to be dimethyl(isopropylphenyl) hydroperoxymethane.

One large group of these hydroperoxymethanes is that group in which each of the three substituent groups is a hydrocarbon radical. One of the sub-groups of these compounds is the alkaryl-dialkyl hydroperoxymethanes, in which the two alkyl groups are relatively short, i. e. have from one to three or four carbon atoms each, including dimethyl(tertiarybutylphenyl) hydroperoxymethane, dimethyl(diisopropylphenyl) hydroperoxymethane, dimethyl isopropylphenyl) hydroperoxymethane, dimethyl(dodecyl phenyl) hydroperoxymethane, dimethyl (methylphenyl)hydroperoxymethane, and corresponding methylethyl and diethyl compounds, and the like. Another subgroup includes at least one long alkyl group directly attached to the hydroperoxymethane, such as methyldecyl(methylphenyl)- hydroperoxymethane, ethyldecylphenylhydroperoxymethane, and the like. Still another group includes trialkyl compounds, such as dimethyldecylhydroperoxymethane, and the like; aralkyl compounds, such as l-phenyl-B-methyl-B-hydroperoxybutane, can also be considered to be members of this group. A further subgroup includes alkyldiaryl compounds, such as methyldiphenylhydroperoxymethane, methylphenyltolylhydroperoxymethane, and the like. A further subgroup is the triaryl compounds, such as triphenyl hydroperoxymethane, tritolyl hydroperoxymethane, and the like. These materials preferably will have a total of not more than thirty carbon atoms per molecule. These hydroperoxide compositions not only give faster polymerization rates when used to eifect emulsion polymerizations, but their use also frequently results in a more uniform reaction rate over a given reaction period than do hydroperoxides heretofore used. These advantages are particularly pronounced at polymerization temperatures below C., and down to polymerization temperatures as low as -30 or 40 C., or lower.

We use the hydroperoxides discussed herein as oxidants in polymerization recipes at low polymerization temperatures, i. e. from about l()o C., or just above the freezing point of water, to well below the freezing point of water, such as 40 C. or lower. The recipe will also include a reductant compound or composition. In some recipes this will be a single compound, or a mixture of homologous compounds, such as hydrazine, ethylenediamine, diethylenetriamine, aminoethylethanolamine, ethylenemethylethylenetriamine, tetraethylenepentamine, and the like. These compounds have the general formula RHN (CI-IXCHXNH) m (CHXCHX) NHR where each R contains not more than eight carbon atoms and is of the group consisting of hy- 4 drogen, aliphatic, cycloaliphatic, aromatic, olefinie, and cycloolenic radicals, and each X contains not more than three carbon atoms and is of the group consisting of hydrogen and aliphatic radicals, m is an integer between 0 and 8, inclusive, and n is an integer of the group consisting of 0 and l and is l when m is greater than 0. Each of the foregoing radicals (other than hydrogen) can be completely hydrocarbon in character, and can be of mixed character when containing six or more carbon atoms, such as alkyl, cycloalkyl, aralkyl, alkaryl groups, and the like, and can also have non-hydrocarbon substituents, some of which will have the effect of making them more water-soluble and less oil hydrocarbon)-soluble; particularly useful non-hydrocarbon substituents include oxygen in the form of hydroxy and ether compounds, sulfur in similar compounds (i. e. mercapto compounds and thioethers) and halogen compounds. In such recipes, such a polyamino compound appears to act as a reductant, and no other activating ingredients, such as compounds of polyvalent-multivalent metals, or reducing ingredients, such as a reducing sugar, need be present in order to obtain satisfactory and rapid polymerization of the monomeric material, even at subfreezing temperatures. The amount of polyamino compound used to obtain optimum results also is dependent upon other ingredients in the recipe. Preferred results are usually obtained with between 0.02 to 5 parts by weight, per 100 parts of monomeric material, of the polyamino compound. In other recipes a composition is used which comprises one compound which is an oxidation catalyst, or activator, and another different compound which is a reductant. The oxidation catalyst is generally selected from a group of materials consisting of compounds of metals such as iron, manganese, copper, vanadium, cobalt, etc. In general it is assumed that the metal must be a multivalent metal and in such a condition that it can change its valence state reversibly. The other ingredient ordinarily present is a reductant, and is usually an organic material such as a reducing sugar or other easily oxidizable polyhydroxy compound. Compounds frequently employed in this capacity are glucose, levulose, sorbose, invert sugar, and the like. The multivalent metal ion of the oxidation catalyst can easily and readily pass from a low valence state to a higher valence state, and vice versa. Sometimes this compound, when present in its lower valence state, can function in the dual role of reductant and oxidation catalyst. One commonly used oxidation catalyst is an iron pyrophosphate, and is separately made up in aqueous solution from a ferrous salt, such as ferrous sulfate, and a pyrophosphate of an alkali metal, such as sodium or potassium.

When a ferrous pyrophosphate activator is used it is preferably prepared by admixing a ferrous salt, such as ferrous sulfate, with a pyrophosphate of an alkali metal, such as sodium or potassium, and water and heating this mixture, preferably for the length of time required for maximum activity. A reaction occurs between the salts, as evidenced by the formation of a grayish-green precipitate. When preparing the activator the mixture is generally heated above 50 C., for variable periods depending upon the temperature. For example, if the mixture is boiled, a period of twenty minutes or less is sufcient to produce the desired activity, and the time of boiling may even be as low as 30 seconds. One convenient method of operation involves maintaining the temperature of the activatorsolution at about, 60'? C. for

a perico lor heatingienging from-1o to lso minutes.

Prior toY heating 'the "activator 'mixture'thevessel I* is usually'lushedlwith aninertgas suchv as nitrogen: In general -it` isl preferred to heat the mix-V turel below'the boilingpoint, say at a temperature aroundl 55l to 75 C'.

Incases where the activator-is prepared just a suitable drying agent, suchA as calcium-chloride;

andin aninert atmosphere such'as'nitrogen. When' usingthis crystalline product inemulsion polymerization reactions; it is generally charged tothe' reactorjust prior to introduction of the butadiene. to be a:4 sodium ferrous pyrophosphate complex, suchas might be exemplified by the formula oir-perhaps NazFePzOi. In anyevent the complex,r whatever its composition, isonly slightly soluble-inwaterand is one active form of ferrous ionandpyrophosphate which can be successfully used in our inventtion. It may be incorporated in/thepolymerization mixture as such, or dissolvedI in sufficient water to produce solution.

Other formsof multivalent'metal and pyrophos-v phatemay also be used, so `long-as there is present-in the reacting mixtureasoluble form of a mu'ltivalent metahcapableof existingin two valencesta-tes and present primarily'inthe lower o1 two vvalence states, and a pyrophosphate.-

The amounts lof activator ingredients `are usually vexpressed in terms of the monomers charged. Theniultivalent-metalshould be within the range of "0.-101ito- 3 millimols per 10U-'parts by weightv of monomer-s, with'0-2 to 2.5 millimols being generally preferred. The amount of pyrophosphate should loe-within the range of 0.10 to 5.6 millimols based on 1GO parts vby weight ofmonomers; however, the-narrower range-oi 0-.2 tof2.5 millimols is more`I frequently preferred. The mol ratio of ferrousV salt to alkalimetal pyrophosphate canbe between 1:0.2 andl:3.5, with a preferred ratio between -1 $.35 and Vl :2.8.

In effecting emulsion' polymerization ofl a monomeric material, particularly when'a batchtype or-sem-i-batch-type operation is carried out, the-reactor is usually first charged with `the aqueousl medium, whichV contains the desired emulsifyingfagent, and the lmonomeric materialis then admixedwith agitation of the contents. sameltime a reaction modifier, such'as a mercaptan, is also included, usually insolutionin at least a partof the monomeric material. solutonland an-oxidant are separately added to the reaction mixture, and reaction then proceeds. A preferred manner of adding these ltwo constituents is usuallyfto have the activator solution incorporated in the aqueous medium prior to addition=of-the monomeric material, and toV add the oxidantas'the last ingredient. Sometimes, however; satisfactory polymerization results can be obtained-when thisprocdure is reversed. It is also-sometimes the practice toA add portions of" one` orz the' otherLA of theV activator "solutions and oxidant intermittently,- or continuously. during This crystalline material is believed At the An activatorl ingredients arefadmixed :in somewhat lthe samey order prior to theirrxnal introduction'intothe. polymerizationv reaction zone:

As previously stated, it; is usuallydesi-rable thatn the multivalentvmetal bepresent; in itsglower valence state. With some recipes, itis unneces- Y sary to include an organic'-reducingjagent.either in the activator solution or inthe polymerization, mixture; However; particularly at temperatures above 0 C., a fasterreaction is .sometimes-'obtained with some-recipes Wlfien-'ffa-smalll amount f of an organic reducingagent, such.l as a .reducing-` sugar," is vincluded vin the r,polymerization recipe, and it is frequently more `desirableto incorporateY this in the reaction system by rst includingrit in the activator solutionr` along withpthe-.other ingredients. When the multivalent ion is present -in its higher valence state; it isusually necessary..

valence state when the activatorsolution is ready,`

for addition to the polymerization mixture.

The monomeric materialfpolymerized:to produce polymers by the processiofIthis-'invention comprises unsaturated organic compounds-which generally contain the characteristic structurel CH2=C and, in mostcasesha-ve at least-,ones of the disconnected valenciesattached to ,an1electronegative group, that yis, agroup. which-increases the polar characterof thezmolecule such:` as a chlorine group or an organic. groupY containing a double or triple bond suchzas vinyl, phenyl, nitrile, carboxy or the like. Includedfin thisclass of monomers are theV conjugated.;butadienes,or, 1,3-butadienes such as butadiene (LBJ-butadiene), 2,3-dimethyl-1,3-butadiene, isoprene, piperylene, 3-furyl-1,3-butadiene, 3-methoxy-L3-butadiene and the like; haloprenes,l sucnasschloroprene- (2-chloro-1,3butadiene) .bromoprene, methylchloroprene (2-ch1oro-3-methyl-l,3butadiene), and the like; aryl olens such as styrene, various alkyl styrenes, p-chlorostyrene, p-methoxystyrene, alpha-methylstyrene, vinylnaphthalene and similar derivatives thereof, and the `like; acrylic and substituted acrylic acids and their, esters, nitriles and amides such as.acrylic acidmeth-- acrylic acid, methyl acrylate, ethyl: acrylate, methyl alp-ha-chloro-acrylate, methyl methacrylate, ethyl methacrylate, butyl methacrylate,y methyl ethacrylate, acrylonitrile, methacrylo-AV nitrile, methacrylamideand `the like; methyl ,isopropenyl ketone, methyl' vinyl ketone, methyl vinyl ether, vinylethinyl alkyl carbinols, vinyl acetate, vinyl chloride, vinylidene chloride, vinylfurane, vinylcar-bazcle, vinylacetylene and other unsaturated hydrocarbons, esters, alcohols, acidaV others, etc., of the types described.v Such. .unsatu-Y rated compounds maybe polymerized alone, in'. which case simple linear. polymers areformect, or mixtures of two-or moreofsuch: compounds which are copolymerizable with eachother in aqueous emulsion may bepolymerizedlto form linear copolymers.

The process of thisinvention is particularlyeffective when the monomeric material polymerized is a polymerizable aliphatic conjugated dioleiin or a mixture of such conjugated diolenzwithz lesser amounts oi one or more other. compounds' containing an active CHz=C igroup Whichare copolymerizable therewith Asuch asfarylf olens; acrylic and substituted acrylic aaicidsfzesters;` ni.-v

triles and amide's, nethyl isopropenyl ketone, vinyl chloride, and similar compounds mentioned hereinabove. In this case the products of the polymerization are high molecular weight linear polymers and copolymers which are rubbery in character and may be called synthetic rubber. Although, as can be readily deduced from the foregoing, there is a host of possible reactants, the most readily and commercially available monomers at present are butadiene itself (L3-butadiene) and styrene. The invention will, therefore, be more particularly discussed and exemplified with reference to these typical reactants. With these specific monomers, it is usually preferred to use them together, in relative ratios of butadiene to styrene between 65:35 and 90:10 by weight.

It is generally preferred that the emulsion be of an oil in Water type, with the ratio of aqueous medium to monomeric material between about 0.5:1 and about 235:1, in parts by weight. It is frequently desirable to include water-soluble components in the aqueous phase, particularly when the polymerization temperatures are below freezing. Inorganic salts and alcohols can be so used. Alcohols which are applicable, when operating at low temperatures, comprise water-soluble compounds of both the monohydric and polyhydric types, and include methyl alcohol, ethylene glycol, glycerine, erythritol, and the like. The amount of alcoholic ingredient used in a polymerization recipe must be suilicient to prevent freezing of the aqueous phase and generally ranges from 20 to 80 parts per 100 parts of monomers charged. In most cases the amount of water employed is suiiicient to make the total quantity of the alcohol-water mixture equal 150 to 200 parts. In cases where it is desired to use a larger quantity of the alcohol-water mixture, say around 250 parts, the amount of alcohol may be increased to as much as 120 parts. It is preferred that the alcohol be such that it is substantially insoluble in the non-aqueous phase, and that 90 per cent, or more, of the alcohol present be in the aqueous phase. A high-boiling alcohol such as glycerine is diiicult to recover from the resulting serum; a low-boiling alcohol such as methanol is easily removed and frequently preferred. Other low-boiling alcohols such as ethanol, however, are frequently too soluble in the liquid monomeric material to permit satisfactory operation. If the resulting latex tends to gel at low reaction temperatures, a larger proportion of aqueous phase should be used. In the practice of the invention suitable means will be necessary to establish and maintain an emulsion and to remove reaction heat to maintain a desired reaction temperature. The polymerization may be conducted in batches, semicontinuously, or continuously. The total pressure on the reactants is preferably at least as great as the total vapor pressure of the mixture, so that the initial reactants will be present in liquid phase. Usually 50 to 98 per cent of the monomeric material is polymerized.

It is one of the outstanding advantages of the use of the hydroperoxides, as disclosed herein, that it is feasible to produce high solids latices i. e. latices resulting from the use of an amount of aqueous medium in the lower part of the range disclosed, i. e. a ratio of aqueous phase to monomeric material between 0.5:1 to 1:1 and an extent of conversion in the higher part of the range disclosed, i. e. from 70 per cent conversion to complete conversion.

Emulsifying agents which are applicable in these low temperature polymerizations are materials such as potassium laurate, potassium oleate, and the like, and salts of rosin acids. Particularly useful are the specic mixtures of salts of fatty acids and of rosin acids, which seem to have a synergistic action when used with some of these same hydroperoxides, as more fully disclosed and claimed by Charles F. Fryling and Archie E. Follett in their application Serial No. 72,534, filed January 24, 1949. However, other emulsifying agents, such as nonionic emulsifying agents, salts of alkyl aromatic sulfonic acids, salts of alkyl sulfates, and the like which will produce favorable results under the conditions of the reaction, can also be used in practicing the invention, either alone or in admixture with soaps. The amount and kind of emulsifier used to obtain optimum results is somewhat dependent upon the relative amounts of monomeric material and aqueous phase, the reaction temperature, and the other ingredients of the polymerization mixture. Usually an amount between about 0.3 and 5 parts per parts of monomeric material will be found to be sufficient.

The pH of the aqueous phase may be varied over a rather Wide range without producing deleterious effects on the conversion rate or the properties of the polymer. In general the pH may be within the range of 9.0 to 12, with the narrower range of 9.5 to 10.5 being most generally preferred.

The mercaptans applicable in this invention are usually alkyl mercaptans, and these may be of primary, secondary, or tertiary configurations, and generally range from Ca to C16 compounds, but may have more or fewer carbon atoms per molecule. Mixtures or blends or mercaptans are also frequently considered desirable and in many cases are preferred to the pure compounds. The amount of mercaptan employed will vary, depending upon the particular compound or 'blend chosen, the operating temperature, the freezing point depressant employed, and the results desired. In general, the greater modification is obtained when operating at low temperatures and therefore a smaller amount of mercaptan is added to yield a product of a given Mooney value, than is used at higher temperatures. In the case of tertiary mercaptans, such as tertiary C12 mercaptans, blends of tertiary C12, C14, and C16 mercaptans, and the like, satisfactory modication is obtained with 0.05 to 0.3 part mercaptan per 100 parts monomers, but smaller or larger amounts may be employed in some instances. In fact, amounts as large as 2.0 parts per 100 parts of monomers may be used. Thus the amount of mercaptan is adjusted to suit the case at hand.

The amount of hydroperoxymethane used to obtain an optimum reaction rate will depend upon the other reaction conditions, and particularly upon the type of polymerization recipe used. The amount is generally expressed in millimols per 100 parts of monomeric material, using in each instance the same units of weight throughout, i. e. when the monomeric material is measured in pounds the hydroperoxymethane is measured in millipound mols. The same is true for other ingredients of the polymerization recipe. An optimum rate of polymerization is usually obtained with the amount of hydroperoxymethane between 0.1 and 19 millimols per 100 parts by weight of monomeric material. The hydroperoxide can frequently be easily separated from accompanying materials by converting it to a ...corresponding saltzof' an alkali metal, .which is usually a crystalline material in a pure orconcentrated state atatmospheric temperatures, and separating the salt. This salt can be used as an .active form of the hydroperoxide, since it is ipromptlyconverted to the hydroperoxide by hyidrolysis when the, salt 'sadmixed'with the-aqueous medium "of the polymerization reaction mixture.

Advantages of thisinventionare illustrated by the following examples. The reactants, 1 and their proportions, and the other specific ingredients ofthe `recipes are presented as beingtypical and should not he construed to limit theinvention unduly. One `of the interestingproperties of those trisubstituted hydroperoxymethanes discussed herein in which the substituent groups are hydrocarbon `radicals is their relatively highdistribution, coefficient ratio. of hydroperoxide dissolved in hydrocarbon phase to hydroperoxide dissolved in the aqueous phase, and the influences of an emulsifying agent'on this-distribution, as

contrasted withi'the distribution coefficient for Such a material as cumene hydroperoxide.

' The distribution of cumene'hydroperoxide and` of 'diisopropylbenzene hydroperoxide between theliquid phases of yaitypical polymerization recipe,.with.and without'soap at 10 C., was investigated' (in the absence of` the usual polymerization catalystactivator). `It'was first es- .tablished that less than two hourswas required 'to reach an equilibrium distribution. The peroxides. were determined by the method of Wagner `et. al.,Anal. Chem., 19,976 (1948). The system employed was the following:

'Butadiene Partsby weight 70 f Styrene do 30 Water -do 180 Methanol ido 40 'Cumene or diisopropylbenzene `Hydroperoxide do 0;20 0.'2l '"*K-laurate (when used) 'do 5.0 Temperature .L '10 The liquid mixtures were agitated at C. for two hours and then allowed to ystand at 10 fC. until phase separation was adequate. The

following data were obtained upon analysis Vof' the hydrocarbon and water phases:

Percent hydroperoxide Hydroperoxide type Parts' v'- '.SQiip HC phase H2O phase v`Cf1 1ir1e11e 0. None l 483 17 Do 0. K laurate.- j V.60 40 f Diisopropy1benzene 0.21 None ,90 10 Do 4 0.21 "Kl laurate.. 79 2l The solubilization of hydroperoxides by soap Butadicne the conventional procedure. 75...

Percent hydroperoxide inw Hydroperoxide type .Parts .Soap

fHiOphase 4 Oumene 0.20 None 90 10 Do. v0.20 K .lauratej 6l 39 Diisopropylbenzene.. 0.20 None 1 92 8 .Do 0; 20 K lauratdj 84 16 The copolymerization of butadiene and styrene was carried out at 10 C. .using the following recipe 70 parts by weight. Styrene.. 30 parts by weight. Water 192 parts by weight. Methanolv 48 parts by Weight. Potassium lauratc. 5.0 parts by weight. Mercoptan blend l 0.25 part by weight.

Dimethyl (isopropylphenyD- 0.15 part by weight (0.7.7.mllimo1). l1ydroperoxy-methane composition 2.

Activator Solution:

Potassium chloride 0.4 part by weight. Frrois sulfate, FeSOl.- 0.2 part byweight (0.72 uiillirnol).

Soldium pyrophosphate, 0.32 part by Weight (0.72millimol).

Na4P2O7.10H2O.

1 A blond ofy tertiary C1?, CM, and Cweliphatiemercaptans in a ratio of3:l:1 parts by Weight.

' l Calculation based on 100 :percent dsopropylbenzenemon hydroperoxide.

In preparing the dimethyl- (isopropylphenyD- hydroperoxy methane (or diisopropylbenzene .hydroperoxide-composition,` a mixture of 200ml.

perature bath maintained at C. Dry oxygen .was `then -passed `through'the 1'eacto1'1and:,the

reactionJmixturewas agitated vigorously. .As

the oxidation proceeded small samples werewithdrawnperiddically'from. the reactor andanalyzed for hydroperoxide content. The oxidation was stopped after two hours Whenthe reaction mixture reached an active oxygen contentof 4.0 per cent or a hydroperoxide. content orf4'7i5Ipe1-"cent, calculated as the monohydroperoxideohm-diiso- -propylbenzene l The contents of the reactor-were then withdrawn immediately, chilled to 0 C., placedjin a suitablel container, and stored-at -|5 C.

The oxidation mixture from thisoxidationfis :made up of unreaeted;mediisopropylbenzene,y the monohydroperoxide of that hydrocarbon, and other oxygenatedproducts. When this mixture was subjected to distillation at 1 2 mm.v pressure and at room temperature, the volatile, nonhydroperoxidic constituents were removed as distillate. `The still-pot residue recovered `vatithe end of the distillation had an active oxygencontent of 4.9y per cent or a hydroperoxide 4content of 58.9 perY cent, calculated as thefmonohydroperoxide of mediisopropylbenzene.

Preparation of the activator compositonffwas eected by dissolving the ferrous sulfate, sodium fpyrophosphate, and potassiumaohloride.inthe requisite quantity of waterandheating ther-resultingmixture at: 60 C. fora() minutes. -Concentrations Vofy ingredients were adjusted in such a way that 25` ml. ofthe activator solution was-usedper loojgrams of monomers charged.

3 Polymerization was carried out "accordingjto A conversion .of "160 per centwas reached inr 6l1ours.

Y Example II The recipe of Example I was followed except that the emulsiiier employed was potassium tetraout a series of butadiene/styrene copolymerizations:

Butadiene 72 parts hy weicht. 28 parts by weight. 180 parts by weicht. Rosin soap, potassium salt, 4.7 parts by weight.

pH l (Dresinate 214). Mercaptan blend 1 0.25 part by weight. Diisoprooylbenzene hydro- Variable.

peroxide composition 1 Potassium hydroxide 0.037 part by weight. Potassium chorde 0.5 part by weicht. Dextrose 1.0 part by Weight. Activator solution:

Potassium pyrophospliate, 0.165 part by weight. (0.50 millimol).

Mols Hydroperoxide Conversion, percent hydro- Run peroxide pclgiol Parts 2 hours 7 hours 12 hours 1 Run 7 was made with 0.1 part cumene hydroperoxide (100 percent) substituted for the diisopropylbenzene hydroperoxide composition.

Example IV The recipe of Example I was followed except that the emulsifying agent employed was the potassium salt of hydrogenated tallow acid. Specifications for this soap are as follows:

Two runs were made at C., the rst one using 0.15 part diisopropylbenzene hydroperoxide (0.77 millimol) and the second employing 0.12 part cumene hydroperoxide (0.78 millimol). In the first run a 60 per cent conversion was reached in 4.6 hours while in the second case a 1,2-hour Not to exceed 6. 1.0% maximum. 2.0% maximum.

12 reaction period was required to reach the same conversion.

Example V A series of butadiene-styrene copolymerizations was carried out using variable amounts of diisopropylbenzene hydroperoxide as the oxidant. The following recipe was employed:

Butadiene 72 parts by weight. Styrene 28 parts by weight. 10 Water 180 parts by weight. Alkyl aryl sufonate 5.0 parts by weight. Mercaptan blend 2 0.24 part by weight. Hydroperoxide Variable. Ferrous sulfate. FeSO4.7H 0.08 part by weight (0.29 millmol). Poltasilm py'rophosphate, 0.101 part by weight (0.31 millimol) 4 2 7. 15 Dextrose 1.00 part by Weight. Potassium hydroxide.-- 0.08 part by weight.

1 Santomerse isopropanol and the resulting slurry heated cooled to 16 C. and filtered to remove any inorganic salts present. The product obtained was extracted with pentane to remove the unsulfonated material and then dried.

1 See Example I.

No. l. The commercial product was treated with to 74 C. It was then A mixture of 5.0 grams of dextrose and 5.0 ml. of 3 per cent potassium hydroxide was made up to 50 ml. with water and digested 11 minutes at 70 C. The requisite quantity of this mixture was then employed in the polymerization recipe.

The activator solution was prepared by dissolving 1.77 gm. potassium pyrophosphate (K4P2O1) in approximately 50 ml. water and adding it to 1.40 gm. ferrous sulfate (FeSO4.7H2O) dissolved in approximately 50 ml. water. The mixture was made up to 100 m1. and heated 23 minutes at 60 C.

The emulsier, water, dextrose solution, and activator were charged to the reactor in the order named after which the mercaptan dissolved in styrene was added. The butadiene was then introduced, the temperature adjusted to 5 C., and the hydroperoxide added. Polymerization was effected at 5 C. using the conventional technique. Results obtained after a 13-hour reaction period in runs containing different amounts of diisopropylbenzene hydroperoxide are shown below together with a control run in which 0.10 part cumene hydroperoxide was substituted for the diisopropylbenzene hydroperoxide.

Conversion, percent 13 hours Two polymerization runs were carried out at C. using the recipe and procedure of Example V except that variable amounts of ferrous sulfate, potassium pyrophosphate, and hydroperoxide were used. A control run was also made in which cumene hydroperoxide was employed as the oxidant. The data are herewith presented.

Hydroperoxide Parts Parts Parts `Hydroperoxide fperiod of 3.25` hours.

A=series of polymerization runswas-carriedvout A:at5""C. using the two..hydroperoxides,:cumene .and diisopropylbenzene, as oxidants f. and `rpotas- ,Butadiene 47,0 parts byyveight. i

Styrene Emulser Mercaptan blend 1 30 parts by Weight. i 170 parts by Weight. 5 parts by weight. 0.25 part by Weight. (See below.)

l0 parts byweizht. 0.14pa1't by Weight.(0.50 millimol).

-Potassium soaps were prepared from the fol- "lowing commerciallyavailable materials.

(1. Neofat D-242: Ahydrogenated-joleic .acid-.1... 4rosin acid mixture.

2. Neofat S142 Reinedhydrogenated tall `oil containing a highpercentage of rosin acid.

3. Indusoil: A mixture containing 55-60 per .cent fatty-acids, it-.3619er` cent rosin-vacidS.' and crystals.

Two-polymerization runs were, made witheach emulsifying agent, one -in Vwhich '0.11' part diisoprOpylbenzenelhydroperoxide (0.57v millimol) Afwas .usedasthe `oxidant andl one infwhich V0.0,8parte 35 variedffrom10i0'i81to30g208 fpart. while the qua-ncumene hydroperoxide (0.53 millimollwas used.

The resultsfare tabulatedV below.

Thesuperiority of diisopropylbenzenehydroper- ..oxide in all'cases-is clearly demonstrated; -anldiiis e.

Tshownrto :be very marked in several cases.

'Example VIII of the potassium salt of;diisopropylbenzeneghydroperoxide per 100` parts ofthe hydrocarbomto be oxidized. -The reaction was continued-rior a The concentration. off hy- 0.165 partby weight (0.50 millirnol). l

14 yof:1.tinarft-luer-'ingredientseywemrzhemrccristant. -A control run using 0.1 part (0.66 millimol) .cumene hydroperoxide was also made. The following tabulation-shows the. results obtained.

20 "The-recipe'offExample III -wasffollowed for. car- '-ryingout a series -0f1-1polymerization runs: except 'that ftertebutylisopropylbenzene Thydroperoxide was lused-as #the-oxidant `Thepreparation .of wvtert-loutylisopropylbenzene Vhydroperoxifie was @.25 eiected byatheoxid'ation-of vtert-butylisopropyl- Y benzene at 1125250. :using as 2in-initiator 0.46 lpart of the potassium salt-of. diisopropylbenzene hy- Ldroperoxide :per '-100 -.parts of the hydrocarbon to abe/:oxidized The reaction -waszallowed .to proceed 3015 hours=-at.-whiclr-time the concentration of hydroperoxide ini .thef mixture'was 16.05 percent. `l?olymerzation:waseiected vat 5 C. usingv the sameprocedure asfthatk given inExample III. In fi'our-runs theaamountxofthe hydroperoxide was ...titiesl of: 'the 'other-i1 ingredients :were held -ecnvetant. A controlrun:u'singOlpart-numeric hydroperoxidewas also made. The-following tabulation shows the results obtained.

The recipe of Example III was followed for carrying outarseries*of;polymerization runs except 'that 1dodecylisopropylbenzene hydroperoxide was used as 'the eoxidant. This Vhydroperoxide was 60 nprepared"loyet-he 0oxidation of dodecylisopropylbenzene,=which hadbeenpreviously-prepared by lat-he'a.l kylation of isopropylhenzenewith l-'dooieccene. 'This dodecyiisopropylben-zene lwas oxidized l:at 1' 130 C.- toc form `dodecylisopropylbenzene rhy- .vn'the Dleeefall initiator-,Comprisinglalparll 65 fd-roperoxide. As anlinitiator'0:9-part-of the-pota'ssium saltof diisoprcpylbenzene' hydroperoxide per 100-parts of `the hydrocarbon `to be oxidized Awas employed. After-- avsix-'hour reaction period the concentration fof-peroxide inthe reaction cent Polymerization was effectedfat 5YC.:using the-samefprocedurezas l thatgiyenirrExampleiil '1,111 Athreerlms the; amount Aof vthe hydroperoxide swasvai'iedfrom; 010.881.150 0.177fpart. (.037&to0.75

millirnol) per 100 parts monomers. .LThe:amounts veffected at 5 C. using-the samejprocedureas that given@ Exampie--III. *In tfou-r runs the amenait i-@fachehydroperoxide was-.Varied from 0.12 to 0:32 fpafrt-whilefthefquarititiesiofstheother'ingredients 75 were=heldf constant. A control-run-Wasalso made.

15 The following tabulation shows the results obtained:

Para methylisopropylbenzene hydroperoxide was prepared by the oxidation of p-methylisopropylbenzene at a temperature of 126 C. using as an initiator one part of the potassium salt of diisopropylbenzene hydroperoxide per 100 parts of the hydrocarbon to be oxidized. The reaction was allowed to proceed for 5.5 hours at which time the concentration of hydroperoxide in the reaction mixture was 14.1 per cent.

The recipe of Example III was followed for carrying out a series of polymerization runs except that p-methylisopropylbenzene hydroperoxide was used as the oxidant. Polymerization was ef fected at C. using the same procedure as that given in Example III. In four runs the amount of hydroperoxide was varied from 0.052 to 0.250 part while the quantities of the other ingredients were held constant. ,A control run using 0.1 part cumene hydroperoxide was also made. The fol lowing tabulation shows the results obtained:

Example XII Meta methylisopropylbenzene hydroperoxide (dimethyl (2 methylphenyl) hydroperoxymethane) was prepared by the oxidation of methylisopropylbenzene containing 60 to 'l0 per cent of the meta compound, 25 to 30 per cent of the para compound and 4 to 'l per cent of the ortho compound. Since the meta-compound predominates, the oxidation product is so designated. Oxidation was effected at 126 C. using as an initiator 0.9 part of the potassium salt of diisopropylbenzene hydroperoxide per 100 parts of the hydrocarbon to be treated. The reaction was allowed to proceed 8.75 hours at which time the concentration of hydroperoxide in the reaction mixture was 14.1 per cent. l

The recipe of Example III was followed for carrying out a series of polymerization runs except that m-methylisopropylbenzene hydroperoxide was used as the oxidant. Polymerization was effected at 5 C. using the same procedure as that given in Example III. In four runs the amount of hydroperoxide was varied from 0.062 to 0.250 part while the quantities cf the other ingredients 5 were held constant. A control run using 0.1 part cumene hydroperoxide was also made. The resuits are herewith presented.

resormzo Hydroperoxide Ciglgn hydro- Mu. P Paris Type Paris mlol Oxtoe 2-hr.5hr.7hr.

0.14--- 0.50 m-Merhyliso- 0.062 0.37 0.75 10.2 29.8 48.0

propylben- Example XIII Dodecyltoluene hydroperoxide (methyl-decyl- (methylphenyl)hydroperoxymethane) was prepared by the oxidation of dodecyltoluene which had been proviously prepared by the alkylation of toluene with l-dodecene. Oxidation was effected at 140 C. using as an initiator 0.5 part of the potassium salt of diisopropylbenzene hydroperoxide per 100 parts of the hydrocarbon to be treated. The reaction was continued for 7 hours at which time the concentration of the hydroperoxide in the reaction mixture was 7.5

er cent.

The recipe of Example III was followed for carrying out a series of polymerization runs except that dodecyltoluene hydroperoxide was used as the oxidant. Polymerization was eiected at 5 C. using the same procedure as that given in Example III. In four runs the amount of hydroperoxide was varied from 0.1'1 to 0.511 part while the quantities of the other ingredients were held constant. A control run using 0.1 part cumene hydroperoxide was also made. The data are herewith presented.

Mol Conversion FeSO4.7H2O Hydroperoxidc ratio percent hydro- M'11 M'u' pmx i 1- 1 li cto Parts mols Type Parts mols FGM, 2-hr. 5-hr. 7hr.

0.14.-. 0.50 Dodecyltoluene 0.11 0.37 0.75 5.9 25.0 37.4 0.14,.- 0.50 do .22 0.75 1.5 13.0 47.2 07.8 0.14 0.50 d 0.365 1.25 2.5 12.6 I10.0 71.2 0.14 0.50 ..do. 0.511 1.75 3.5 0.0 18.8 34.4 0.14,-- 0.50 Cumenc 0.10 0.60 1.3 7.8 24.5 36.0

Example XIV assegno Cumelrdroper Iglo Conversion, percent.

Y hydroperoxide i Parts Millimols to Fe 2 hrs. 5 hrs. 7 hrs. 12 hrs. 24 hrs.

0.038 0. 25 0. 5' 11.6 2S. S 42. 6 02. 4 71. 4 0.057. 0. 375 0. 75 11.2 29. 2 40; 4 G9. 0 89. 0 0.076-.- 0. 50 l. 0` 9. 9 27. 8 40.' 7 69. 9 i 93. b 0.10 0. 66 1. 3 9.8 2513 38. 7 69. 3 93. 2 0.15 0. 99 2j 0` 9. 4 24`. 0 36. 0 67: 7 93. 5

It is interestingV to notel that, in this specic recipe, there is little variation of conversion, with the relative amount of cumene hydroperoxide over an appreciable range. In contrast, not only; does thev use of the other hydroperoxides give faster rates, but the ratesf showa more defined variation with the relative amount of' hydroperoxide.

A series of runs `Nas made in which dii'erent hydroperoxides were employed as oxidants in the following polymerization recipe:

Butadiene styrene... Water, totaL Soap 11akes Potassium chloride Mercaptan blend 1;.. 'Tetraethylcncpentamine Oxidant 1 See Example I.

parts by Weght. 7 0

A mixture or" the emulsifying agent, Water, and potassium chloride Was prepared and' potassium hydroxide added to adjust the pH to 10.3., A solue` tion of the hydroperoxide and mercaptan in styrene was then introduced followed 'oy the butadiene. The reactor was pressured tor 30 pounds per equa-reinen gauge With nitrogen andthe temperature adjusted to- C. Sufficient Water Wasiadded to the tetraethylenepentarnine to make a solution and this mixture was then charged to the reactor. vPolynfierization was effected in the conventional manner While the temperature was held at 5 C. A control run was also made using cumene hydroperoxide as the oxidant. Results from the various runs aretabulated below.

Example XVI A series of polymerizations was carried out at 10 C. using different emulsiers in the following tert-hutylisopropylbenzene hydroperoxideltetraetl'iylenepentarnine recipe:

Butadiene 70 parts by Weight. Styrene 30'parts by Weight. Water, total- 192 parts by weight. ethanol 48 parts by Weight. Potassium ohlov idc 0.4 part bywelsht.

Mercaptan blend 1 h A Tert-butylisopropylbon 0.4/2 part by Weight (2.27 mrlhmols).

Tetraethylenepentamine 0.275 part by Weight (1.5 millimols).

5.0 parts by Weight. 0.1 partby Weight.

1 See Example I.

A mixture `of Vthe emulsifying agent, pater,

y the tetraethylenepentamine to make a solution Mercaptan. blend j and thismixturewas then charged toy thereaotor. Polymerization Was carried out in the conventional manner with the temperature being held at -10 C. The results are herewith presented:

pHl ofr Conversion, percent Emulsiei" Parts tion 2 hrs. 4 hrs. 7'hrs. 2l hrs. osinsoap,Ksalt- 5;() 10.25 0 1 I 2y 9 osiu soap 2. 3. 5 f Soap flakes 2 1'. 5 1014 I 8 18 32 1 86 D0.3 5. 0 10. l 7 13 19; 52 K lagere.. 5. o 11.0 17 se 1 9s o 2. 5 v K myristate 2. 5 11' 6 a 24 43 69 98 1 Dresnate 214, 2 Dresinate 2l4/K-SF flakes. 3 K-SF Hakes.

10 C. to study the eiect of varying the pH in the following recipe:

Butadene. parts by weizht. Sty-rene 30 parts by weight. Water. 192 parts by Weight. Methanol. 48 parts by weight. Rosin soon. 3.5 partsbyY weight.

Fatty acid soa 1.5 parts by Weight. i

0.25 part by Weight 0.416 part by weight (2 millimols).

T e rtbutylisopr n hydroperoxide. Tetraethylenepentamine 1.50 parts by weight. Potassium chloride 0.25 part by weight. Potassium hydroxide. Variable.

1 Dresinate 214/K-SF flakes. 2 See Example I.

The pH, the quantity of 1.04 N potassium'hydroxide added, and the time-conversion data are shown below. A control run was made using cumene hydroperoxide in place of tert-butylisopropylbenzene hydroperoxide and these data are also presented,

Tert-butyllsopro T etraethylcne- Conversion, pgfdgy' pentairfine Mol ratio percent hydro- Y, peroxide] Miiiiiiiiiiamm@ 4 24 Parts mois Parts mois hrs. hrs. hrs.

3. 0. 5 2. 64 1. 14 Z1. 0 34 57 79 2. 1. 0 5. 30 0. 47 :1. 0 37 62 90 2. 0 1. 5 7. 95 0. 25 Il. 0 37 60 75 l. 5 2. 0 10. 55 0.14 :1. 0 35 49 52 1.0 2. 5 13 20 0. 0761].0 30 38 42 0. 5 3. 0 15. 80 0. 063:1. 0 2l 23 23 Example XIX Several ethylene amino compounds were employed as activators in the following polymerization recipe:

l See Example I.

The procedure of Example XV was followed with the temperature of polymerization being held at 5 C. The following results were obtained:

Conversion, percent Amino compound 3.5 hrs. 7 hrs. 24 hrs.

Ethylencdiamine.. 5 7 60 Dictbylenetriamine. l5 28 76 Triethylenetetramiii 48 73 96 Tetraethylenepentain' 80 Example XX A polymerization run was made using the recipe of Example XIX, except that sec-propylenediamine (1,2-diaminopropane) was employed as the activator. The following time-conversion Aminoethylethanolamine was used as the activator in the polymerization recipe of Example XIX. A conversion of 60 per cent was reached in 24 hours.

Example XXII The recipe of Example XIX was employed when carrying out a polymerization reaction at 5 C. using hydrazine, added as hydrazine hydrate, as the activator. A conversion of 16 per cent was reached in 24 hours.

Example XXIII A series of polymerization runs was carried out at 10 C. using the following recipe:

Tetraetbyleriepentamino. Variable. Potassium chloride 0.25 part by weight.

l Dresinate 214. I K-SF flakes. l See Example I.

In all runs the millimol ratio of hydroperoxide to amine was 0.5: l but the initiator level was varied. The following results were obtained:

20 Millimol Conversion percent Time to pgjirge Amine, level 60% conparts parts hydrpversion,

peroxide 4.0 hrs. 6.5 hrs. 24.0 hrs. hours 0.06 0. 095 0. 12 24 70 15.0 25 0.12.-.- 0.19 0. 50 17 33 77 12. 2 0.18.-.- 0.28 0.75 24 42 8l 10. 0 0.24.-- 0. 38 l. 00 28 49 87 8. 2 0.31... 0.47 1.25 33 54 91 7.2 0.35. 0.57 1. 50 33 56 92 0. 8 0.47- 0. 76 2.0 3G 58 ill 0. 5 0.59 0.95 2. 5 37 60 94 6. 4

Example XXIV Parts by weight Butadiene 70 Styrene 30 0 Water '75 Fatty acid soap 1 0.5 Sodium alkyltoluene sulfonate 1.0 Rosin soap, potassiumsalt2 1.5 Sodium salt of condensed alkyl aryl sulfonic acid3 0.25

Mercaptan blend4 0.4 Diisopropylbenzene h y d r o p e r o x i d e (100%) 0.15 Potassium ch1oride 0.5

Potassium hydroxide 0.05

Activator composition:

FeSOMHzO 0.14 K4P207 0.177 Dextrose 1.0

Booster solution:

Water 5 Potassium chloride 0.1

Potassium hydroxide 0.06

xlotasislum Ofilce Rubber Reserve soap.

00 2Dresiniite 214.

aDaxad-ll.

4 See Example I.

For the preparation of the activator composition, the dextrose and potassium pyrophosphate 05 were rst dissolved in 10 parts water and the `ijiczz'mpfze XXV The copolymeriaation wof butadiene` with styrene Was` eiected at' 5 C. according tor the-following recipe:

1 .As in Example XXIV.

The sani- 'riargng prece-dere 'as da 'given in the preceding example employed; al1. ingrefets bein@ intredacjed mitral-1y; A ez'perfcent slids' latex was obtained'v 27 hours.

xample XXV- Affi'g'h solids latex was prepared 'at 55;" using the follo'wing polymerization recipe:

Parts by Weight FGSL'I-IZO ';.Y Y KlzPzfO ma ain mama-'e xine. 'The activator composition waspreparedgas follvrs: lthe 4'ferrous sulfate was dissolved. in rparts Water and the potassium pyrophosphate added. The mixture was dilated with fiY parts Water, .H'eat'edfto 605' C.,`and cooled to room temperature before being used.L y 4,

The `'charg'ing V'procedure x'gi-rer; in Example Afterfporymeaet n had a'its weight Water 2. 5

Tert-butylsopropylbenzene hy- 0. 104 0. 104 0. 104

droperoxide.

Tetraethylenepentamin 0.189-

1 As in raniple The reactorwas purged with nitrogen and the jvvate'r. "emulsier; Mixad- '11, potassiumhydroxide, and potassiumchloride charged. This mixture `was previouslyheate'd to 50-60 C". to dissolve all ingredients and Was cooled to room temperature prior to being charged. The pH of this solution was 1118 'TheH temperature was A'next adjusted to- 5 C; Vand'a mixturer of the amine in three parts Water Wasnt'roduced. A solution of the `mercapt'anii'rstyre'ne was addedfollowed by the butadiene-after Which the temperature was adjusted again to 5 C. andthe hydroperoxide nally introduced. The reactor'Was then pressured to 30 `pounds per square inch 'gauge with nitrogen. After a reaction time of 42.2 hours the latex "contained 44.3 per lcent solids. -At this point the conversion had reached '75.7 per cent.

Example- XXVIII Diisprcpiflchlrobenzene (100 parts), prepared by th alkylatioii of chlrobenzene with propylene under conditions such as to add two isopropyl gicips to th'eben'zene nucleus,v was'y charged to a reactor, together with 1;'6 parts of the potassium salt cil tert-butylisoprpylbenzenenhydroperoxide. heated t'o 1310" QL, andoxygen introduced at a controlledrategfvor a tivo-hour period Whil'efthe 'I'ri'zrture vvas agitated. `'At the conclusion of the reaction the`cpncntration of resulting monohydrop'eroifide invth reaction in'i'iiture was 17.0 p 'er cent. This aterial Was employed as the oxidant, in a seriesuo'f polyrneriation runs at 5 C. 'SiIg the fllowing. vrecipe:

Disoppylchlorb ...ide ma Potassium hyd V 'lfctassiun-chloridav Y A Dektrse a 1.0 Activator cnbcsltin:

193297; ed FeSOeHH 11i at summatietwa ee Example i.

Variable with the amounts of hydroperoxide employed..

For purposes of comparison, a control run was made using cumene hydroperoxide in an amount previously found to be optimum for this recipe.

Hydroperoxide FeSOMHzO Mols Conversion, percent hydrovru' w11' 'gem-1 ii i i- 1 e mo Parts lmlols Parts mois F v 2 hrs. 5 hrs. 7 hrs.

0.0s5. 0. 375 0.14 0.5 0. 75 30. 3 73. 4 8s. 7 0.114 '0.5 0.14 0.5 1.0 30.1 79.4 92.0 0.172 0.75 0.14 0.5 1. 5 28.1 76.4 90.8 0.228. 1. 0. 14 0. 5 2.0 24. 8 74. 6 89. 9 0.1 1. 0. 66 0.14 0.5 1.3 I 12. 5 29. 5 42. 0

l Cumene hydroperoxide (control).

As will be evident to those skilled in the art, various modifications of this invention can be made, or followed, in the light of the foregoing disclosure and discussion, without departing from the spirit or scope of the disclosure or from the scope of the claims.

We claim:

1. In the production of synthetic rubber by the polymerization of a monomeric material comprising a major portion of 1,3-butadiene and a minor portion of styrene while dispersed in an aqueous emulsion in the presence of a catalyst composition at a polymerization temperature, the improvement which comprisesccnducting said polymerization with the pH of said aqueous emul- Ysion between 9 and 12 andlusing as said catalyst composition 0.1 to 10 millimols of dimethyl- (tertiary butylphenyl) hydroperoxymethane together with 0.02 to parts of tetraethylenepentamine, said amounts being per 100 parts by weight of said monomeric material.

2. In the production of synthetic rubber by the polymerization of a monomeric material comprising a major portion of 1,3-butadiene and a minor portion of styrene while dispersed in an aqueous emulsion in the presence of a catalyst composition at a polymerization temperature, the improvement which comprises conducting said polymerization with the pH of said aqueous emulsion between 9 and 12 and using-as said catalyst composition 0.1 to millimols of dimethyl- (isopropylphenyl)hydroperoxymethane together with 0.02 to 5 parts of tetraethylenepentamine, said amounts being per 100 parts by weight of said monomeric material.

3. In the production of synthetic rubber bythe polymerization of a monomeric material comprising a major portion of 1-,3-butadiene and a minor portion of styrene while dispersed in an aqueous emulsion in the presence of a catalyst compositionat a polymerization temperature, the improvement which comprises conducting said polymerization -with the `pH ofgsaid Aaqueous emulsion between 9 and 12 and using as said catalyst composition 0-.1 `to 10 millimols or dimethyl- 24 (diisopropylphenyl) hydroperoxymethane together with 0.02 to 5 parts of tetraethylenepentamine, said amounts being per 100 parts by weight of said monomeric material.

4. In the production of synthetic rubber by the 4polymerization of a monomeric material comprising a major portion of 1,3-butadiene and a minor portion of styrene while dispersed in an aqueous emulsion in the presence of a catalyst composition at a polymerization temperature, the improvement which comprises conducting said polymerization with the pH of said aqueous emulsion between 9 and 12 and using as said catalyst composition 0.1 to 10 millimols of dlmethyl tertiary butylphenyl) hydroperoxymethane together with 0.02 to 5 parts of aminoethylethanolamine, said amounts being per parts by weight of said monomeric material.

5. In the polymerization of a monomeric material comprising an organic compound having an active CH2=C group at a polymerization temperature while dispersed in an aqueous medium in the presence of a polymerization catalyst comprising an oxidant and a reducing composition, the improvement which comprises using as said oxidant 0.1 to 10 millimols of a trisubstituted hydroperoxymethane having 10 to 30 carbon atoms per molecule and as said reducingcomposition 0.02 to 5 parts of a polyamino compound having the formula RHN(CHXCHXNH) m (CHXCHX) NI-IR where each R contains not more than eight carbon atoms and is of the group consisting of hydrogen, aliphatic, cycloaliphatic, aromatic, olefinie, and cycloolenic radicals, and each X contains not more than three carbon atoms and is of the group consisting of hydrogen and aliphatic radicals, m is an integer between 0 and 8, inclusive, and n is an integer of the group consisting of 0 and 1 and is 1 when m is greater than 0, said amounts being per 100 parts by weight of said monomeric material.

6. The process of claim 5 in which said hydroperoxymethane is dimethyl(disopropylchlorophenyl) -hydroperoxymethane- 7. In the polymerization of a monomeric material comprising an organic compound having an active CH2=C group at a polymerization temperature While dispersed in an aqueous medium in the presence of a polymerization catalyst comprising an oxidant and a reducing composition, the improvement which comprises using as said oxidant 0.1 to 10 millimols of dimethyl(tertiary butylphenyl)-hydroperoxymethane and as said activating-reducing composition 0.02 to 5 parts of tetraethylenepentamine, said amounts being per 100 parts by weight of said monomeric material.

8. In the polymerization of a monomeric material comprising an organic compound having an active CHz:C group at a polymerization temperature while dispersed in an aqueous medium in the presence of a polymerization catalyst comprising an oxidant and a reducing composition, the improvement which comprises using as said oxidant 0.1 to 10 millimols of dimethyl- (isopropylphenyl)hydroperoxymethane and as said activating-reducing composition 0.02 to 5 parts of tetraethylenepentamine, said amounts being per 100 parts by Weight of said monomeric material.

9. In the polymerization of a monomeric material 'comprising an organic compound having an active CH2=C group at a polymerization temperature while dispersed in an aqueous medium in the presence of a polymerization catalyst comprising an oxidant and a reducing composition, the improvement which comprises using as said oxidant 0.1 to 10 millimols of dimethyl diisopro pylphenyl)hydroperoxymethane and as said activating-reducing composition 0.02 to parts of tetraethylenepentamine, said amounts being per 100 parts by Weight of said monomeric material. 10. An improved process for producing synthetic rubber, which comprises establishing and maintaining at a polymerization temperature not higher than C. a dispersion of an aqueous phase, a liquid monomeric material comprising a major amount of 1,3-butadiene and a minor amount of styrene, an emulsifying agent, a reaction modifier, 0.1 to 10 millimols of a trisubstituted hydroperoxymethane containing 10 to 30 carbon atoms per molecule, and 0.02 to 5 parts of a polyamino compound having the formula Where each R contains not more than eight carbon atoms and is of the group consisting of hydrogen, aliphatic, cycloaliphatic, aromatic, olenic, and cycloolenic radicals, and each X contains not more than three carbon atoms and is of the group consisting of hydrogen and aliphatic radicals, m is an integer between 0 and 8, inclusive, and n is an integer of the group consisting of 0 and 1 and is 1 when m is greater than 0, said amounts being per 100 parts by Weight of said monomeric material.

11. The process of claim 10 in which said hydroperoxymethane is dimethyl(isopropylphenyl)hydroperoxymethane.

12. The process of claim 10 in which said hydroperoxymethane is dimethyl(tertiarybutylphenyl) hydroperoxymethane.

13. The process of claim 10 in which said hydroperoxymethane is dimethyl diisopropylphen y1) hydroperoxymethane.

14. An improved process for producing a polymeric material of high molecular weight, which comprises establishing and maintaining at a polymerization temperature a dispersion of an aqueous phase, a liquid monomeric material comprising an organic compound having an active CH2=C group and polymerizable when dispersed in an aqueous emulsion, an emulsifying agent. a trisubstituted hydroperoxymethane containing 10 to 30 carbon atoms per molecule, and a polyamino compound having the formula Where each R contains not more than eight carbon atoms and is of the group consisting of hydrogen, aliphatic, cycloaliphatic, aromatic, olenic, and cyclooleiinic radicals, and each X contains not more than three carbon atoms and is of the group consisting of hydrogen and aliphatic radicals, m is an integer between 0 and 8, inclusive, and n is an integer of the group consisting of 0 and 1 and is 1 when m is greater than 0, said amounts being per parts by weight of said monomeric material.

15. An improved process for producing synthetic rubber, which comprises establishing and maintatining at a polymerization temperature not higher than 10 C. a dispersion of an aqueous phase, a liquid monomeric material comprising a major amount of 1,3-butadiene, an emulsifying agent, a reaction modifier, 0.1 to 10 millimols of dimethyl (isopropylchlorophenyl) hydroperoxymethane, and 0.02 to 5 parts of tetraethylenepentamine, said amounts being per 100 parts by Weight of said monomeric material.

16. An improved process for producing synthetic rubber, which comprises establishing and maintaining at a polymerization temperature not higher than 10 C. a dispersion of an aqueous phase, a liquid monomeric material comprising a major amount of 1,3-butadiene and a minor amount of styrene, an emulsifying agent, a reaction modier, 0.1 to 10 millimols of a trisubstituted hydroperoxymethane containing 10 to 30 carbon atoms per molecule, and 0.02 to 5 parts of tetraethylenepentamine, said amounts being per 100 parts by weight of said monomeric material.

WILLIAM B. REYNOLDS. JOHN E. WICKLATZ. THOMAS J. KENNEDY.

Shearon, Jr. et al.: Ind. & Chem., May 1948, pp. 769-777. 

1. IN THE PRODUCTION OF SYNTHETIC RUBBER BY THE POLYMERIZATION OF A MONOMERIC MATERIAL COMPRISING A MAJOR PORTION OF 1,3-BUTADIENE AND A MINOR PORTION OF STYRENE WHILE DISPERSED IN AN AQUEOUS EMULSION IN THE PRESENCE OF A CATALYST COMPOSITION AT A POLYMERIZATION TEMPERATURE, THE IMPROVEMENT WHICH COMPRISES CONDUCTING SAID POLYMERIZATION WITH THE PH OF SAID AQUEOUS EMULSION BETWEEN 9 AND 12 AND USING AS SAID CATALYST COMPOSITION 0.1 TO 10 MILLIMOLS OF DIMETHYL(TERTIARY - BUTYLPHENYL) - HYDROPEROXYMETHANE TOGETHER WITH 0.02 TO 5 PARTS OF TETRAETHYLENEPENTAMINE, SAID AMOUNTS BEING PER 100 PARTS BY WEIGHT OF SAID MONOMERIC MATERIAL. 